Selective hydrogenation catalyst for unsaturated compound

ABSTRACT

The present invention relates to a selective hydrogenation catalyst for an unsaturated compound. The supported catalyst contains at least one Group VIB non-noble metal oxide and at least one Group VIII non-noble metal oxide deposited on a carrier; and the catalyst has an optimized acid distribution on the surface of the catalyst, and more preferably has an optimized Group VIII/VIB metal ratio and a Group VIII non-noble metal density per unit of catalyst surface area. Using the catalyst of the present invention can have the following advantages: the weight increase of light sulphides in an unsaturated compound or a mixture containing unsaturated compounds, the hydrogenation of a polyunsaturated compound, the isomerization of a monounsaturated compound, high operation flexibility and a significant improvement in the effects of a hydrogenation treatment.

FIELD OF TECHNOLOGY

The present invention relates to a selective hydrogenation catalyst for an unsaturated compound.

BACKGROUND ART

During a selective hydrogenation process for unsaturated compounds, the raw materials may contain certain amounts of sulphides in addition to the unsaturated compounds, and all of the sulphides or portion of them are light sulphides. These light sulphides can react with polyunsaturated compounds in the raw materials under the action of a hydrogenation catalyst to generate heavy sulphides, which can be removed by a process of fractionation.

The polyunsaturated compounds in the raw materials as described above have very unstable properties and are easy to be polymerized during storage and subsequent processing. Under the action of the hydrogenation catalyst, a portion of the polyunsaturated compounds can be selectively hydrogenated into monounsaturated compounds.

At the time of hydrogenating the polyunsaturated compounds into monounsaturated compounds, a small portion of the polyunsaturated compounds or monounsaturated compounds are hydrogenated into saturated compounds, and the occurrence of such reaction can be avoided as much as possible by optimized design for the catalyst.

CN03815240.1 proposes a method for selective hydrogenation of polyunsaturated compounds into monounsaturated compounds using a homogeneous catalyst. This method uses at least one salt of a transition metal element from Groups IB, IIB, VB, VIB, VIIB and VIII of the periodic table, at least one ligand and at least one organometallic reducing agent.

CN200610064286.5 proposes a method of selective hydrogenation using a catalyst having controlled porosity. The method uses a catalyst on a carrier, comprising at least one metal from Group VIB and at least one non-noble metal from Group VIII used in the sulphurized form, deposited on the carrier and having a controlled porosity, wherein: the weight content of Group VIB element oxide is necessarily higher than 12% by weight; the weight content of Group VIII element oxide is lower than 15% by weight; the sulphurization degree of metal components in the catalyst is at least equal to 60%; and the pore volume having a diameter larger than 0.05 microns in the catalyst is 10˜40% of total pore volume.

CN200610064287.x proposes a method for selective hydrogenation employing a sulphurized catalyst. The method uses a catalyst deposited on a carrier and comprising at least one metal from Group VIB and at least one non-noble metal from Group VIII, wherein: the weight content of Group VIB element oxide is necessarily higher than 12% by weight; the weight content of Group VIII element oxide is lower than 15% by weight; the sulphurization degree of metal components in the catalyst is at least equal to 60%; and the molar ratio of the non-noble metal from Group VIII to the metal from Group VIB is 0.2˜0.5 mole/mole.

CN200610064397.6 proposes a method of selective hydrogenation using a catalyst with a specific carrier. The method uses a supported catalyst comprising at least one metal from Group VIB and at least one non-noble metal from Group VIII used in the sulphurized form, deposited on a specific carrier comprising a metal aluminate of the MAl₂O₄ type with a metal M selected from nickel and cobalt.

CN200910170584.6 proposes a method for selective hydrogenation using a sulphurized catalyst with a specified composition. The catalyst comprises at least one metal from Group VIB and at least one non-noble metal from Group VIII supported on alumina, wherein: the Group VIB metal oxide is 4˜20% by weight of the catalyst; the Group VIII non-noble metal oxide is less than 15% by weight of the catalyst; the molar ratio of the non-noble metal from Group VIII to the metal from Group VIB is 0.6˜3.0 mole/mole; and the catalyst has a total pore volume of 0.4˜1.4 cm³/g.

SUMMARY OF THE INVENTION

The object of the present invention is to provide a selective hydrogenation catalyst for an unsaturated compound, which may result in increase of light sulphides weight and isomerization reaction of monounsaturated compounds, in addition to selective hydrogenation.

A selective hydrogenation catalyst for an unsaturated compound, which is a supported catalyst, characterized in that at least one Group VIB metal and at least one Group VIII non-noble metal are supported on a carrier, wherein:

-   -   the amount by weight of the Group VIB element oxide is 4˜10%,         preferably 6˜8%;     -   the amount by weight of the Group VIII non-noble element oxide         is 6˜15%, preferably 8˜12%;     -   the ratio B_(total)/L_(total) of B acid to L acid in the surface         acidity center of the catalyst is not more than 0.4, preferably         0.05˜0.3;     -   the ratio L_(weak)/L_(strong) of weak L acid to strong L acid in         the surface acidity center of the catalyst is 0.5˜2.0,         preferably 0.5˜1.5; and     -   the carrier is or substantially is alumina.

In the present invention, the molar ratio of the Group VIII non-noble metal oxide to the Group VIB metal oxide in the catalyst is preferably more than 3.0 and equals to or less than 5.0 mole/mole, especially from 3.2 to 5.0 mole/mole; the density of the Group VIII element per unit surface area of the catalyst is not less than 8×10⁻⁴ g of Group VIII element oxide/m² of catalyst, especially not less than 10×10⁻⁴ g of Group VIII element oxide/m² of catalyst, by virtue of which the effect is better.

Under the action of the acidity center of a catalyst, the unsaturated compounds in processed raw materials tend to take polymerization reaction to produce raw coke precursors such as colloids and the like, and these substances would cover the surface activity center of the catalyst, impacting on the exertion of catalytic action. However, as for reaction of sulphides weight increase and isomerization reaction, the catalyst is further required to have a certain acidity center. As a result, in the design of a catalyst, in order to meet the requirements of various reactions, it is necessary to adjust the constitution of acidity center of the catalyst and distribution of strong, weak acidity centers.

The methods for adjusting the ratio of B acid to L acid and the ratio of weak L acid to strong L acid in the surface acidity center of the catalyst are not limited in the present invention. Methods of this aspect are also described in the book “Hydrogenation process and engineer”, China Petrochemical Press, for instance, modification of carriers by using non-metal oxides, hydrothermal treatment of catalyst carriers, and the like. The present invention could employ, but not limited to, the methods described therein. Therefore, the composition of a carrier is not particularly limited in the present invention, provided that the ratio of B acid to L acid and the ratio of weak L acid to strong L acid specified in this invention can be satisfied. The carrier recommended in this invention is or substantially is alumina. The content of alumina is preferably not less than 80 wt %, more preferably not less than 90 wt %. According to different materials to be treated, variety of alumina can be selected in terms of crystal forms, total pore volumes and specific surfaces. Preferably, the crystal form of alumina is γ, δ, θ or a mixed crystal thereof. As for different carrier compositions, the adjustment method of the surface acidity centers thereof can be varied, which is a basic means of carrier modification. In addition to “Hydrogenation Technology and Engineering”, there are numerous literatures that relate to methods for adjusting the surface acidity center of a carrier, such as those in CN102039151, CN1597093 and the like. Thus, the requirement of a carrier to have a specific surface acidity center has been completely achieved in the prior art, and manufacturers can provide corresponding products depending on the users' needs. For instance, a well-known method in the art is used to prepare a catalyst carrier: as needs, the carrier can be modified with non-metal oxides or precursors, and the resulting carrier can either be treated with water vapor at 400˜600° C. for 4˜6 h, or be calcinated at a temperature of 500˜700° C. or 700˜900° C. or 900˜1100° C. for 4˜6 h. By this method, the properties of the acidity center of the catalyst and the distribution of strong/weak acid centers can be adjusted. Preferably, the total pore volume of the catalyst is 0.2˜0.5 cm³/g, more preferably 0.2˜0.45 cm³/g, and most preferably 0.2˜0.39 cm³/g. Preferably, the specific surface of the catalyst is 50˜200 m²/g, more preferably 50˜150 m²/g.

From the study on the hydrogenation reaction system of unsaturated compounds or mixtures containing the unsaturated compounds, the inventors found that the effect of hydrogenation treatment is improved notably when the catalyst has the features defined according to the present invention.

Pyridine infrared analysis is used to analyze the acidity center of the catalyst. This method is described in detail in “Modern Research Methods of Catalysis” published by Science Press, in chapter 7, in-situ infrared spectroscopy. As for other parameters, well-known analysis and calculation methods in the art are used.

Various technical means, such as tableting, mixing and kneading, ball milling, extrusion, spraying-forming and the like, can be used to prepare a catalyst carrier. The catalyst carrier can be modified by various technical means to satisfy the requirement for the properties of the catalyst in this method.

The preparation method for a catalyst is not particularly limited in the present invention, and general impregnation methods can be employed, for example, the salts of active components (nickel and/or molybdenum) can be added into water or another solution, capable of forming complexes, to produce an active metal impregnating solution. The catalyst carrier was impregnated in the active metal impregnating solution, and then dried at 120˜300° C. and calcinated at 400˜800° C.

The present invention increases the conversion rate and the selectivity for hydrogenation of a polyunsaturated compound, and increases the isomerization ratio of a monounsaturated compound, by means of selecting active components of a catalyst, optimizing acid distribution on the surface of the catalyst, especially further selecting suitable Group VIII/VIB metal ratio for the catalyst and a density of Group VIII non-noble metal per unit surface area of the catalyst. Isomerized olefins often have higher stabilities and octane values, which are usually very important to improve the properties of the unsaturated compounds or the mixtures containing the unsaturated compounds.

Like the prior art, when being used, the catalyst needs to be sulphurized under the same sulphurization conditions as in the prior art, for example, metal oxides were conversed to sulfides. Typically, sulphurization is carried out under the following sulphurization conditions: a pressure of 0.5˜3.0 MPa; a sulphurization temperature of 200˜500° C.; a sulphurization space velocity of 0.5˜5.0 h⁻¹; and an atmosphere of hydrogen, hydrogen sulfide.

The conditions for using the catalyst can be: a pressure of 1.0˜5.0 MPa; a hydrogen/polyunsaturated compound molar ratio of 1˜20 mole/mole; a space velocity of 2.0˜6.0 h⁻¹; and a temperature of 50˜250° C.

When the unsaturated compounds or the mixtures containing the unsaturated compounds are treated by using the catalyst of the present invention, the treatment is allowed to operate at a relative higher hydrogen/polyunsaturated compound molar ratio (e.g., more than 5.0), and the degree by which the monounsaturated compounds are hydrogenated into saturated compounds is very low, which results in large operation flexibility.

In a process of selective hydrogenation for unsaturated compounds, several reactions (included without limitation thereto) may take place as follows:

(1) Addition Reaction of Polyunsaturated Compounds:

Since polyunsaturated compounds are highly active and tend to take addition reactions with other compounds to produce compounds having larger molecular weights. When sulfides, in particular light sulfides, are included in the reaction system, sulfides having higher boiling points can be produced by utilizing the addition reactions of polyunsaturated compounds, and such sulfides can be removed by a process of fractionation.

(2) Selective Hydrogenation of Polyunsaturated Compounds into Monounsaturated Compounds:

Under the action of a catalyst, the polyunsaturated compounds can be selectively hydrogenated into monounsaturated compounds.

(3) Isomerization of Monounsaturated Compounds:

During the process of hydrogenation, monounsaturated compounds can take an isomerization reaction, which contributes to improve the stability of the monounsaturated compounds.

(4) Hydrogenation of Monounsaturated Compounds:

At the time of hydrogenation of polyunsaturated compounds into monounsaturated compounds, a small portion of the monounsaturated compounds are hydrogenated into saturated compounds. In most instances, it is desirable for the monounsaturated compounds to be retained. As a result, the monounsaturated compounds are required to be hydrogenated to minimum level by optimization of catalysts and conditions.

DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS

In the present invention, important technical parameters for evaluating catalyst performance are expressed as follows: conversion rate of propanethiol %=(1−propanethiol content in product/propanethiol content in raw material)*100 conversion rate of dienes %=(1−dienes content in product/dienes content in raw material)*100 conversion rate of monoenes %=(1−monoenes content in product/monoenes content in raw material)*100 isomerization rate of monoenes %=isomerized olefins content/(isomerized olefins content+alkanes content)*100 hydrogenation selectivity %=conversion rate of dienes/(conversion rate of dienes+conversion rate of monoenes)*100

COMPARATIVE EXAMPLE 1

100 g of industrial grade SiO₂—Al₂O₃ powder (SiO₂ content: 14%) was added with 50 g of water, and then was subjected to kneading and extrusion molding. The resultant was then dried at 120° C. and calcinated at 600° C. for 4 h to produce a catalyst carrier.

14 g of industrial grade ammonium molybdate was added into 45 g of water, and stirred to be dissolved. Next, 75 g of industrial grade nickel nitrate, 12 g of industrial grade citric acid were added thereto and stirred to be dissolved, to produce an active metal impregnating solution for catalyst.

The catalyst carrier was added into this impregnating solution, impregnated at normal temperature for 3 h. After that, the impregnated catalyst carrier was taken out and aged for 12 h, then dried at 120° C. and calcinated at 500° C. for 4 h to produce Catalyst A. This catalyst has a specific surface of 149 m²/g, a total pore volume of 0.41 cm³/g, MoO₃ content of 6.4% and NiO content of 10.6%. More data for property analysis are shown in Table 1.

COMPARATIVE EXAMPLE 2

100 g of industrial grade alumina powder was added with 50 g of water, and then was subjected to kneading and extrusion molding. The resultant was then dried at 120° C. and calcinated at 500° C. for 4 h to produce a catalyst carrier.

14 g of industrial grade ammonium molybdate was added into 45 g of water, and stirred to be dissolved. Next, 75 g of industrial grade nickel nitrate, 12 g of industrial grade citric acid were added thereto and stirred to be dissolved, to produce an active metal impregnating solution for catalyst.

The catalyst carrier was added into this impregnating solution, impregnated at normal temperature for 3 h. After that, the impregnated catalyst carrier was taken out and aged for 12 h, then dried at 120° C. and calcinated at 500° C. for 4 h to produce Catalyst B. This catalyst has a specific surface of 240 m²/g, a total pore volume of 0.38 cm³/g, MoO₃ content of 6.4% and NiO content of 10.6%. More data for property analysis are shown in Table 1.

COMPARATIVE EXAMPLE 3

100 g of industrial grade alumina powder was added with 50 g of water, and then was subjected to kneading and extrusion molding. The resultant was then dried at 120° C. and calcinated at 500° C. for 4 h, and was further calcinated at 900° C. for 4 h to produce a catalyst carrier.

11 g of industrial grade ammonium molybdate was added into 80 g of water, and stirred to be dissolved. Next, 40 g of industrial grade nickel nitrate, 12 g of industrial grade citric acid were added thereto and stirred to be dissolved, to produce an active metal impregnating solution for catalyst.

The catalyst carrier was added into this impregnating solution, impregnated at normal temperature for 3 h. After that, the impregnated catalyst carrier was taken out and aged for 12 h, then dried at 120° C. and calcinated at 500° C. for 4 h to produce Catalyst C. This catalyst has a specific surface of 101 m²/g, a total pore volume of 0.38 cm³/g, MoO₃ content of 5.0% and NiO content of 5.8%. More data for property analysis are shown in Table 1.

COMPARATIVE EXAMPLE 4

100 g of industrial grade alumina powder was added with 50 g of water, and then was subjected to kneading and extrusion molding. The resultant was then dried at 120° C. and calcinated at 500° C. for 4 h, and was further calcinated at 900° C. for 4 h to produce a catalyst carrier.

30 g of industrial grade ammonium molybdate was added into 90 g of water, and stirred to be dissolved. Next, 30 g of industrial grade nickel nitrate, 12 g of industrial grade citric acid were added thereto and stirred to be dissolved, to produce an active metal impregnating solution for catalyst.

The catalyst carrier was added into this impregnating solution, impregnated at normal temperature for 3 h. After that, the impregnated catalyst carrier was taken out and aged for 12 h, then dried at 120° C. and calcinated at 500° C. for 4 h to produce Catalyst D. This catalyst has a specific surface of 101 m²/g, a total pore volume of 0.38 cm³/g, MoO₃ content of 11.0% and NiO content of 4.0%. More data for property analysis are shown in Table 1.

EXAMPLE 1

100 g of industrial grade alumina powder was added with 50 g of water, and then was subjected to kneading and extrusion molding. The resultant was then dried at 120° C. and calcinated at 500° C. for 4 h, and was further calcinated at 900° C. for 4 h to produce a catalyst carrier.

14 g of industrial grade ammonium molybdate was added into 45 g of water, and stirred to be dissolved. Next, 75 g of industrial grade nickel nitrate, 12 g of industrial grade citric acid were added thereto and stirred to be dissolved, to produce an active metal impregnating solution for catalyst.

The catalyst carrier was added into this impregnating solution, impregnated at normal temperature for 3 h. After that, the impregnated catalyst carrier was taken out and aged for 12 h, then dried at 120° C. and calcinated at 500° C. for 4 h to produce Catalyst E. This catalyst has a specific surface of 101 m²/g, a total pore volume of 0.38 cm³/g, MoO₃ content of 6.4% and NiO content of 10.6%. More data for property analysis are shown in Table 1.

EXAMPLE 2

100 g of industrial grade alumina powder was added with 50 g of water, and then was subjected to kneading and extrusion molding. The resultant was then dried at 120° C. and calcinated at 500° C. for 4 h, and was further treated in water vapor at 450° C. for 4 h to produce a catalyst carrier.

18 g of industrial grade ammonium molybdate was added into 45 g of water, and stirred to be dissolved. Next, 95 g of industrial grade cobalt nitrate, 16 g of industrial grade citric acid were added thereto and stirred to be dissolved, to produce an active metal impregnating solution for catalyst.

The catalyst carrier was added into this impregnating solution, impregnated at normal temperature for 3 h. After that, the impregnated catalyst carrier was taken out and aged for 12 h, then dried at 120° C. and calcinated at 500° C. for 4 h to produce Catalyst F. This catalyst has a specific surface of 97 m²/g, a total pore volume of 0.35 cm³/g, MoO₃ content of 9.1% and CoO content of 14.8%. More data for property analysis are shown in Table 1.

EXAMPLE 3

100 g of industrial grade SiO₂—Al₂O₃ powder (SiO₂ content: 1.4%) was added with 50 g of water, and then was subjected to kneading and extrusion molding. The resultant was then dried at 120° C. and calcinated at 700° C. for 4 h to produce a catalyst carrier.

12 g of industrial grade ammonium molybdate was added into 120 g of 25% aqueous solution of ammonia, and stirred to be dissolved. Next, 75 g of industrial grade nickel nitrate was added thereto and stirred to be dissolved, to produce an active metal impregnating solution for catalyst.

The catalyst carrier was added into this impregnating solution, impregnated at normal temperature for 1 h. After that, the impregnated catalyst carrier was taken out and aged for 12 h, then dried at 120° C. and calcinated at 500° C. for 4 h to produce Catalyst G. This catalyst has a specific surface of 96 m²/g, a total pore volume of 0.42 cm³/g, MoO₃ content of 6.3% and NiO content of 11.7%. More data for property analysis are shown in Table 1.

EXAMPLE 4

100 g of industrial grade SiO₂—Al₂O₃ powder (SiO₂ content: 7%) was added with 50 g of water, and then was subjected to kneading and extrusion molding. The resultant was then dried at 120° C. and calcinated at 600° C. for 4 h to produce a catalyst carrier.

12 g of industrial grade ammonium metatungstate was added into 45 g of water, and stirred to be dissolved. Next, 75 g of industrial grade nickel nitrate, 12 g of industrial grade citric acid were added thereto and stirred to be dissolved, to produce an active metal impregnating solution for catalyst.

The catalyst carrier was added into this impregnating solution, impregnated at 60° C. for 30 min. After that, the impregnated catalyst carrier was taken out and aged for 12 h, then dried at 120° C. and calcinated at 500° C. for 4 h to produce Catalyst H. This catalyst has a specific surface of 142 m²/g, a total pore volume of 0.39 cm³/g, WO₃ content of 7.0% and NiO content of 11.5%. More data for property analysis are shown in Table 1.

EXAMPLE 5

100 g of industrial grade TiO₂—Al₂O₃ powder (TiO₂ content: 3.5%) was added with 50 g of water, and then was subjected to kneading and extrusion molding. The resultant was then dried at 120° C. and calcinated at 500° C. for 4 h, and was further calcinated at 700° C. for 4 h to produce a catalyst carrier.

14 g of industrial grade ammonium molybdate was added into 45 g of water, and stirred to be dissolved. Next, 100 g of industrial grade nickel nitrate, 15 g of industrial grade citric acid were added thereto and stirred to be dissolved, to produce an active metal impregnating solution for catalyst.

The catalyst carrier was added into this impregnating solution, impregnated at normal temperature for 3 h. After that, the impregnated catalyst carrier was taken out and aged for 12 h, then dried at 120° C. and calcinated at 500° C. for 4 h to produce Catalyst I. This catalyst has a specific surface of 165 m²/g, a total pore volume of 0.28 cm³/g, MoO₃ content of 5.6% and NiO content of 13.2%. More data for property analysis are as shown in Table 1.

TABLE 1 Composition and Physical properties of Catalysts A, B, C, D, E, F, G, H and I Catalyst No. Comparative Example Example 1 2 3 4 1 2 3 4 5 A B C D E F G H I Carrier: SiO₂ Al₂O₃ Al₂O₃ Al₂O₃ Al₂O₃ Al₂O₃ SiO₂ SiO₂ TiO₂ (20%)—Al₂O₃ (2%)—Al₂O₃ (10%)—Al₂O₃ (5%)—Al₂O₃ Total pore 0.41 0.38 0.38 0.38 0.38 0.35 0.42 0.39 0.28 volume cm³/g Specific 148 240 101 101 101 97 96 142 165 surface m²/g MoO₃% 6.4 6.4 5.0 11.0 6.4 9.1 6.3 5.6 NiO % 10.6 10.6 5.8 4.0 10.6 11.7 11.5 13.2 WO₃% 7.0 CoO % 14.8 Molar ratio of 3.2 3.2 2.2 0.7 3.2 3.1 3.6 5.0 4.5 Group VIII metal/Group VIB metal d_(Group VIII element oxide) 0.7 0.4 0.6 0.4 1.1 1.5 1.2 0.8 0.8 (10⁻³ g/m²) B_(total)/L_(total) 0.47 0 0 0 0 0 0.06 0.28 0 L_(weak)/L_(strong) 0.8 2.3 1.2 1.2 1.2 2.0 0.6 0.8 0.7

Among these catalysts, catalysts E, F, G, H and I are the catalysts of the present invention. In contrast, catalysts A, B, C and D do not belong to the catalysts of the present invention.

INDUSTRIAL APPLICABILITY EXAMPLE 6 Evaluation of Catalysts

A catalyst is charged into the middle part of a reaction tube having an inner diameter of 15 mm and a height of 320 mm, of which the upper and lower parts are filled with quartz sand of 20˜40 mesh for supporting.

The catalyst is sulphurized before use. The sulphurizing oil is a mixture of cyclohexane and carbon disulfide (CS₂ content is 2%). Sulphurization conditions are: a pressure of 2.0 MPa; a liquid hourly space velocity of 4 h⁻¹; a hydrogen-to-oil volume ratio of 200:1; a temperature of 320° C.; and a sulphurization time of 12 h.

The mixture of unsaturated compounds for testing has the following composition: 100 ppm by weight of propanethiol; 1% by weight of pentadiene; 3% by weight of 1-heptylene; and balance of cyclohexane.

Hydrogenation treatment was performed under the conditions of a pressure of 2.0 MPa, a space velocity of 4 h⁻¹, a temperature of 120° C., and a hydrogen/diene molar ratio of 5:1. Next, the contents of propanethiol, dienes, monoenes, isomerized monoenes and alkanes in hydrogenated products were analyzed.

Hydrogenation experiments were performed by using each of the catalysts of Comparative Examples 1˜4 and Examples 1˜5, and experimental results are obtained and shown in Table 2.

TABLE 2 Experimental results of respective Comparative Examples and Examples Catalyst No. A B C D E F G H I Conversion rate of 100 99.0 98.0 98.5 100 100 100 100 99.0 propanethiol % Conversion rate of 87.2 85.1 75.7 82.7 88.5 88.5 89.5 89.8 87.8 dienes % Isomerization rate 51.3 35.6 32.6 45.6 52.5 52.8 53.7 54.1 51.5 of monoenes % Hydrogenation 95.8 96.6 97.1 97.6 98.5 99.0 99.5 99.3 98.0 selectivity %

In the hydrogenation experiments of unsaturated compounds or mixtures containing unsaturated compounds, the method of the present invention has higher conversion rates of propanethiol and dienes, and isomerization rates of monoenes and hydrogenation selectivities are also apparently higher than those of the method in the Comparative Examples.

EXAMPLES 7˜9

The experiment reactions were performed by using the Catalyst E in Catalyst Example 1, utilizing the same sulfuration method with feedstock of identical composition, and changing reaction conditions, the experimental results obtained are as shown in Table 3.

TABLE 3 Experimental results of Catalyst E under different conditions Example 6 7 8 Catalyst No. E E E Pressure MPa 1.5 2.0 3.0 Space velocity h⁻¹ 2.0 4.0 3.0 Temperature ° C. 100 120 110 Hydrogen/diene 10.0 5.0 15.0 molar ratio Conversion rate of 100 100 100 propanethiol % Conversion rate of 89.2 88.5 88.2 dienes % Isomerization rate 53.1 52.5 52.7 of monoenes % Hydrogenation 99.1 98.5 98.7 selectivity %

As can be seen from the above data, the catalyst illustrated in Example 1 has a good adaptability. The hydrogenation treatment of unsaturated compounds with this catalyst can result in significantly high conversion rate of reaction products and selectivity in a wide range of conditions.

EXAMPLES 10˜12 Effect of Total Pore Volume

In accordance with the method of Example 1, three industrial grade alumina powders having different pore volumes were selected to prepare catalysts respectively, resulting in Catalysts E, J, and K. The major distinction among these three catalysts is being different in total pore volume. The total pore volumes of Catalysts E, J, and K are 0.38 cm³/g, 0.28 cm³/g, and 0.55 cm³/g, respectively. The catalysts were evaluated by the method of Example 6, and resulting experimental results are as shown in Table 3.

TABLE 3 Effect of total pore volume of catalyst Example 10 11 12 Catalyst No. E J K Conversion rate of 100 100 100 propanethiol % Conversion rate of 88.5 88.7 88.2 dienes % Isomerization rate 52.5 53.5 48.7 of monoenes % Hydrogenation 98.5 99.3 97.2 selectivity %

As can be seen from the experimental data, when the total pore volume of a catalyst is suitably reduced, the selectivity of hydrogenation for an unsaturated compound is further improved.

When the catalyst of the present invention is used to hydrogenate unsaturated compounds, the effect of hydrogenation treatment is improved notably. The catalyst of the present invention has higher conversion rate of thiols, higher saturation rate of dienes and better hydrogenation selectivity for dienes as compared to other catalysts. 

What is claimed is:
 1. A selective hydrogenation catalyst for an unsaturated compound, which is a supported catalyst, comprising at least one Group VIB metal component and at least one Group VIII non-noble metal component supported on a carrier, wherein: the Group VIB metal component comprises a Group VIB metal oxide in an amount of from 4% to 10% by weight of the catalyst; the Group VIII metal component comprises a Group VIII non-noble metal oxide in an amount of from 6% to 15% by weight of the catalyst; the catalyst comprises a B_(total)/L_(total) acid strength ratio of Bronsted acid to Lewis acid in a surface acidity center of not more than 0.4; and a L_(weak)/L_(strong) acid strength ratio of weak Lewis acid to strong Lewis acid in the surface acidity center of 0.5 to 2.0; and the carrier is substantially alumina.
 2. The selective hydrogenation catalyst according to claim 1, wherein the Group VIII non-noble metal oxide and the Group VIB metal oxide are in a molar ratio of from greater than 3.0 mole/mole to 5.0 mole/mole; and the Group VIII metal oxide per unit surface area of the catalyst is 8×10⁻⁴ g/m² or greater.
 3. The selective hydrogenation catalyst according to claim 2, wherein the molar ratio of the Group VIII non-noble metal oxide to the Group VIB metal oxide in the catalyst is from 3.2 mole/mole to 5.0 mole/mole.
 4. The selective hydrogenation catalyst according to claim 1, wherein the Group VIB metal component comprises molybdenum, tungsten, or combinations thereof.
 5. The selective hydrogenation catalyst according to claim 1, wherein the Group VIII non-noble metal component comprises nickel, cobalt, or combinations thereof.
 6. The selective hydrogenation catalyst according to claim 1, wherein the Group VIB metal oxide is in an amount of from 6% to 8% by weight of the catalyst.
 7. The selective hydrogenation catalyst according to claim 1, wherein the Group VIII non-noble metal oxide is in an amount of from 8% to 12% by weight of the catalyst.
 8. The selective hydrogenation catalyst according to claim 1, wherein the Group VIII metal oxide per unit surface area of the catalyst is 10×10⁻⁴ g/m² or greater.
 9. The selective hydrogenation catalyst according to claim 1, wherein the acid strength ratio B_(total)/L_(total) of Bronsted acid to Lewis acid in the surface acidity center of the catalyst is from 0.05 to 0.3.
 10. The selective hydrogenation catalyst according to claim 1, wherein the acid strength ratio L_(weak)/L_(strong) of weak Lewis acid to strong Lewis acid in the surface acidity center of the catalyst is from 0.5 to 1.5.
 11. The selective hydrogenation catalyst according to claim 1, comprising a total pore volume of from 0.2 to 0.5 cm³/g.
 12. The selective hydrogenation catalyst according to claim 1, comprising a specific surface of from 50 to 200 m²/g.
 13. The selective hydrogenation catalyst according to claim 1, wherein the amount of alumina in the carrier is not less than 80 wt %.
 14. The selective hydrogenation catalyst according to claim 1, wherein the alumina comprises a crystal form selected from γ, δ, θ, and combinations thereof.
 15. The selective hydrogenation catalyst according to claim 1, wherein the Group VIB metal component comprises molybdenum.
 16. The selective hydrogenation catalyst according to claim 1, wherein the Group VIII non-noble metal component comprises nickel.
 17. The selective hydrogenation catalyst according to claim 1, comprising a total pore volume of from 0.2 to 0.45 cm³/g.
 18. The selective hydrogenation catalyst according to claim 1, comprising a total pore volume of from 0.2 to 0.39 cm³/g.
 19. The selective hydrogenation catalyst according to claim 1, comprising a specific surface of from 50 to 150 m²/g.
 20. The selective hydrogenation catalyst according to claim 1, wherein the amount of alumina in the-carrier is not less than 90 wt %. 